CN113511777A - Chemical industry park comprehensive sewage treatment system and process - Google Patents

Chemical industry park comprehensive sewage treatment system and process Download PDF

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Publication number
CN113511777A
CN113511777A CN202110568580.4A CN202110568580A CN113511777A CN 113511777 A CN113511777 A CN 113511777A CN 202110568580 A CN202110568580 A CN 202110568580A CN 113511777 A CN113511777 A CN 113511777A
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sewage
fenton
treatment
pool
unit
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蒋和凯
宗兴兴
郑刚
杨峰
戴建军
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Jiangsu Nanda Huaxing Environmental Protection Technology Co ltd
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Jiangsu Nanda Huaxing Environmental Protection Technology Co ltd
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    • CCHEMISTRY; METALLURGY
    • C02TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02FTREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F9/00Multistage treatment of water, waste water or sewage
    • CCHEMISTRY; METALLURGY
    • C02TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02FTREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F1/00Treatment of water, waste water, or sewage
    • CCHEMISTRY; METALLURGY
    • C02TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02FTREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F1/00Treatment of water, waste water, or sewage
    • C02F1/001Processes for the treatment of water whereby the filtration technique is of importance
    • CCHEMISTRY; METALLURGY
    • C02TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02FTREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F1/00Treatment of water, waste water, or sewage
    • C02F1/28Treatment of water, waste water, or sewage by sorption
    • C02F1/283Treatment of water, waste water, or sewage by sorption using coal, charred products, or inorganic mixtures containing them
    • CCHEMISTRY; METALLURGY
    • C02TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02FTREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F1/00Treatment of water, waste water, or sewage
    • C02F1/46Treatment of water, waste water, or sewage by electrochemical methods
    • C02F1/461Treatment of water, waste water, or sewage by electrochemical methods by electrolysis
    • C02F1/467Treatment of water, waste water, or sewage by electrochemical methods by electrolysis by electrochemical disinfection; by electrooxydation or by electroreduction
    • C02F1/4672Treatment of water, waste water, or sewage by electrochemical methods by electrolysis by electrochemical disinfection; by electrooxydation or by electroreduction by electrooxydation
    • CCHEMISTRY; METALLURGY
    • C02TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02FTREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F1/00Treatment of water, waste water, or sewage
    • C02F1/52Treatment of water, waste water, or sewage by flocculation or precipitation of suspended impurities
    • CCHEMISTRY; METALLURGY
    • C02TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02FTREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F1/00Treatment of water, waste water, or sewage
    • C02F1/52Treatment of water, waste water, or sewage by flocculation or precipitation of suspended impurities
    • C02F1/5281Installations for water purification using chemical agents
    • CCHEMISTRY; METALLURGY
    • C02TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02FTREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F1/00Treatment of water, waste water, or sewage
    • C02F1/66Treatment of water, waste water, or sewage by neutralisation; pH adjustment
    • CCHEMISTRY; METALLURGY
    • C02TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02FTREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F1/00Treatment of water, waste water, or sewage
    • C02F1/72Treatment of water, waste water, or sewage by oxidation
    • CCHEMISTRY; METALLURGY
    • C02TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02FTREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F1/00Treatment of water, waste water, or sewage
    • C02F2001/007Processes including a sedimentation step
    • CCHEMISTRY; METALLURGY
    • C02TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02FTREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F3/00Biological treatment of water, waste water, or sewage
    • C02F3/30Aerobic and anaerobic processes

Abstract

The invention discloses a chemical industrial park comprehensive sewage treatment system and a process, and belongs to the technical field of sewage treatment. The invention discharges the sewage after the sewage is treated by a grid, a regulating tank, an electrochemical oxidation tower, a Fenton tank, a UBF tank, an A/O tank, a secondary sedimentation tank, a high-efficiency sedimentation tank and an active carbon adsorption tower in sequence, the biodegradability of the sewage is improved while the refractory organic matters are degraded by a front-end advanced oxidation process, a high-quality living environment is provided for the microorganisms subjected to the back-end biochemical treatment, and meanwhile, an active carbon adsorption unit is arranged at the tail end to be used as the guarantee of the standard discharge of the sewage, so that the invention is very suitable for treating the comprehensive sewage of a chemical industrial park with large water quality and water quantity fluctuation, difficult degradation and poor biodegradability.

Description

Chemical industry park comprehensive sewage treatment system and process
Technical Field
The invention belongs to the technical field of sewage treatment, and particularly relates to a chemical industrial park comprehensive sewage treatment system and a process.
Background
With the continuous development of chemical industry economy, the development mode of regional chemical industry enterprises has become one of the main trends of the development of the global chemical industry. According to statistics, by the end of 2019, 676 chemical industry parks are important in China, and according to the prediction of a research institute of the Chinese commercial industry, the number of the chemical industry parks in 2020 can be developed to about 800. Therefore, a large amount of comprehensive sewage generated in chemical industry parks in China is urgently needed to be treated.
In the existing built chemical industry parks in China, although part of the early-built chemical industry parks have sewage treatment plants for centralized treatment of park sewage, the early design and construction of most park sewage treatment plants are carried out by referring to the operation process of urban domestic sewage treatment plants, and the traditional combined process of coagulation and biochemistry (A) is mainly adopted2the/O process, the oxidation ditch process and the SBR process) as main processes for treating the comprehensive chemical wastewater. However, the comprehensive sewage of the chemical industry park is the sewage discharged after a plurality of chemical enterprises in the park pass through the sewage stations in the enterprises for biochemical treatment, and the sewage has the characteristics of large water quality change fluctuation, low biodegradability, high biotoxicity and the like, so that the sewage plant of the chemical industry park built by using the mode of the urban domestic sewage plant is rarely applicable to actual sewage treatment, and phenomena of unstable operation facilities, collapse of an operation system, over-standard water quality of a discharge port and the like often exist.
Therefore, the conventional biochemical process is only adopted to treat the comprehensive sewage of the chemical industrial park, and the requirement of stable standard-reaching discharge of the sewage is extremely difficult to achieve. And aiming at the characteristics of the comprehensive sewage in the chemical industrial park, the sewage can be stably and efficiently discharged after reaching the standard only by improving the biodegradability of the sewage and enhancing the load impact resistance of the sewage treatment process. In summary, the development of novel treatment systems and processes for realizing stable standard discharge of chemical comprehensive sewage is a difficult problem which needs to be solved urgently at present.
Disclosure of Invention
1. Problems to be solved
The invention provides a system and a process for treating chemical industry park comprehensive sewage, aiming at the problems that the prior art has poor treatment effect on the sewage treatment of the chemical industry park and the sewage is difficult to reach the stable standard and discharge. The sewage sequentially passes through a regulating device, an electrochemical oxidation unit, a Fenton treatment unit, a biochemical treatment unit and/or an activated carbon adsorption unit, and the electrochemical oxidation method and the Fenton method are adopted to degrade part of difficultly-degraded COD in the sewage and simultaneously improve the biochemical performance of the sewage; then advanced treatment is carried out through a biochemical process, so that pollutants in water are further degraded; and an activated carbon adsorption method is combined to be used as an emergency guarantee, so that pollutants in the sewage can be further removed deeply, and the sewage is ensured to be discharged up to the standard.
2. Technical scheme
In order to solve the problems, the technical scheme adopted by the invention is as follows:
the invention discloses a chemical industrial park comprehensive sewage treatment system which comprises an electrochemical oxidation unit, a Fenton treatment unit and a biochemical treatment unit, wherein the Fenton treatment unit is arranged between the electrochemical oxidation unit and the biochemical treatment unit, and the front end of the electrochemical oxidation unit is provided with an adjusting device which is connected with the electrochemical oxidation unit through a pipeline; wherein the content of the first and second substances,
the bottom of the electrochemical oxidation unit is provided with a water distribution device, more than two electrochemical packing layers are arranged in the electrochemical oxidation unit, the top of the electrochemical oxidation unit is provided with an internal circulation pipeline, and the top of the electrochemical oxidation unit is connected with the water distribution device through the internal circulation pipeline;
a Fenton dosing area, a Fenton reaction area and a coagulation reaction area are arranged in the Fenton treatment unit, the Fenton reaction area is arranged between the Fenton dosing area and the coagulation reaction area, an aeration device is arranged in the Fenton reaction area, and stirring devices are arranged in the Fenton dosing area and the coagulation reaction area;
the biochemical treatment unit comprises a UBF pool, an A/O pool, a secondary sedimentation pool and a high-efficiency sedimentation pool in sequence, wherein the UBF pool is connected with the Fenton treatment unit through a pipeline, a bracket suspension type packing area is arranged in the UBF pool, and more than two triangular weir plates are arranged at the top of the UBF pool; and is
A plurality of sewage mixing areas are arranged in the adjusting device, guide walls are arranged in the sewage mixing areas, and flow pushers are arranged at positions on two sides of each guide wall.
Preferably, the A/O pool comprises an anoxic pool and an aerobic pool, wherein a filler layer is arranged in the anoxic pool and accounts for 45-60% of the volume of the anoxic pool.
Preferably, the secondary sedimentation tank is of a radial flow sedimentation tank structure, and a mud scraper is arranged in the secondary sedimentation tank.
Preferably, a flocculation dosing area and a phosphorus removal dosing area are arranged in the high-efficiency sedimentation tank.
Preferably, in the Fenton treatment unit, the volume ratio of the Fenton dosing area to the Fenton reaction area to the coagulation reaction area is (1-1.5): (7-10): (1-1.5).
More preferably, in the fenton treatment unit, the volume ratio of the fenton dosing zone to the fenton reaction zone to the coagulation reaction zone is 1: 7: 1.
preferably, the distance between the stirring devices arranged in the Fenton dosing area and the coagulation reaction area and the bottom is 20 cm.
Preferably, the height of a bracket suspension type filler area arranged inside the UBF tank is 2.5-3 m.
Preferably, the adjusting device is provided with a grating in front, and the gap of the grating is 16-25 mm.
Preferably, the chemical industry park comprehensive sewage treatment system further comprises an activated carbon adsorption unit, the activated carbon adsorption unit is connected with the efficient sedimentation tank through a pipeline, an activated carbon packing layer is arranged in the activated carbon adsorption unit, the height of the activated carbon packing layer is 1.5-2.0 m, and the activated carbon adsorption unit is provided with a backwashing pipeline.
The invention relates to a comprehensive sewage treatment process for a chemical industrial park, which comprises the steps of filtering sewage by a grating to remove impurities in the sewage; the filtered sewage enters a regulating device for uniform water quality mixing treatment to obtain sewage with uniform water quality; the sewage with uniform water quality enters an electrochemical oxidation unit for electrochemical oxidation treatment, and macromolecular organic matters in the sewage are decomposed into micromolecular organic matters; the sewage after electrochemical oxidation treatment enters a Fenton treatment unit for Fenton treatment, so that refractory organic matters in the sewage are further removed, the water quality load of the sewage is reduced, and favorable conditions are provided for back-end biochemical treatment; and then the sewage after Fenton treatment enters a biochemical treatment unit, and is subjected to biochemical treatment in a UBF pool, an A/O pool, a secondary sedimentation pool and a high-efficiency sedimentation pool in sequence to obtain the sewage which reaches the discharge standard.
Preferably, the comprehensive sewage treatment process for the chemical industrial park, disclosed by the invention, further comprises the step of enabling the sewage subjected to biochemical treatment to enter an activated carbon adsorption unit for adsorption treatment to obtain the sewage which reaches the standard and is discharged.
Preferably, the hydraulic retention time of the sewage in the electrochemical oxidation unit is controlled to be 2-3 h, the pH value of the sewage in the electrochemical oxidation treatment reaction process is controlled to be 2.5-4, and the reflux ratio of the sewage is controlled to be 50-150%.
Preferably, the reaction time of the sewage in the Fenton reaction zone is controlled to be 3-5 h, the pH value in the reaction process is controlled to be 3-4, and the mass ratio of the adding amount of the oxidant added in the Fenton adding zone to the water inflow of the system is controlled to be (0.8-2.5): 1000.
Preferably, the hydraulic retention time of the sewage in the UBF pool is controlled to be 18-24 hours, the hydraulic retention time of the sewage in the anoxic pool is controlled to be 8-9 hours, and the hydraulic retention time in the aerobic pool is controlled to be 16-19 hours.
Preferably, the sewage reflux ratio in the A/O pool is controlled to be between 150% and 300%, and the sludge reflux ratio between the secondary sedimentation pool and the A/O pool is controlled to be between 50% and 150%.
Preferably, the flocculation reagent added into a flocculation reagent adding area arranged in the high-efficiency sedimentation tank is one or two of PAC (polyaluminium chloride) and PAM (polyacrylamide), wherein the mass ratio of the adding amount of the flocculation reagent to the water inflow of the system is controlled to be (0.8-1): 100000; the phosphorus removal agent added in the phosphorus removal agent adding region is a calcium chloride solution with the concentration of 40%, and the mass ratio of the adding amount of the phosphorus removal agent to the water inflow of the system is controlled to be (0.5-1.5): 1000.
3. advantageous effects
Compared with the prior art, the invention has the beneficial effects that:
(1) the invention relates to a chemical industrial park comprehensive sewage treatment system, which comprises an electrochemical oxidation unit, a Fenton treatment unit and a biochemical treatment unit, wherein the Fenton treatment unit is arranged between the electrochemical oxidation unit and the biochemical treatment unit, the front end of the electrochemical oxidation unit is provided with a regulating device, the regulating device is connected with the electrochemical oxidation unit through a pipeline, the biochemical treatment unit sequentially comprises a UBF (UBF-based pool), an A/O (anoxic/oxic) pool, a secondary sedimentation pool and a high-efficiency sedimentation pool, and after sewage is treated by an electrochemical oxidation method, a Fenton method and a biochemical process, the quality of effluent stably reaches the first-level A discharge standard in pollutant discharge standard GB18918-2002 table 1 of urban sewage treatment plant;
(2) the chemical industrial park comprehensive sewage treatment system has the advantages of load impact resistance, high biological toxicity resistance, high efficiency, stability and the like, occupies small area, has low operation cost and provides technical support for environmental management of the park area in China;
(3) according to the comprehensive sewage treatment process for the chemical industrial park, parameters such as the adding amount of the oxidant, the pH value, the adding amount of the flocculating agent, the adding amount of the phosphorus removal agent, the sewage reflux ratio, the sludge reflux ratio and the like in the process are adjusted, so that the load impact resistance of the process and the operation management efficiency of a sewage plant are improved.
Drawings
FIG. 1 is a schematic flow diagram of a chemical industrial park integrated wastewater treatment process of the present invention;
FIG. 2 is a schematic view of the structure of the adjusting device of the present invention;
FIG. 3 is a schematic diagram of the structure of an electrochemical oxidation unit according to the present invention;
FIG. 4 is a schematic structural diagram of a Fenton treatment unit according to the present invention;
FIG. 5 is a schematic diagram of the structure of a UBF pool of the present invention;
FIG. 6 is a schematic top view of a UBF pool of the present invention;
FIG. 7 is a schematic view of the structure of an activated carbon adsorption unit of the present invention;
in the figure:
100. an electrochemical oxidation unit; 110. a water distribution device; 120. an electrochemical filler layer;
130. an internal circulation pipe; 200. a Fenton processing unit; 210. a Fenton dosing area;
220. a Fenton reaction zone; 230. a coagulation reaction zone; 240. an aeration device; 250. a stirring device;
310. a UBF pool; 3110. a support suspended filler zone; 3120. a triangular weir plate;
400. an adjustment device; 410. a sewage mixing zone; 4110. a guide wall; 4120. a flow impeller;
500. an activated carbon adsorption unit; 510. an active carbon filler layer; 520. and (4) backwashing the pipeline.
Detailed Description
The invention is further described with reference to specific examples.
As shown in fig. 1, the chemical industrial park comprehensive sewage treatment system of the present invention comprises an electrochemical oxidation unit, a fenton treatment unit and a biochemical treatment unit, wherein the fenton treatment unit is arranged between the electrochemical oxidation unit and the biochemical treatment unit, and the front end of the electrochemical oxidation unit is provided with a regulating device which is connected with the electrochemical oxidation unit through a pipeline; the front end of the adjusting device can be further provided with a grating, and the gap of the grating is 16-25 mm. The comprehensive sewage of the chemical industrial park can filter out impurities with smaller particle sizes in the sewage through the grating so as to ensure the normal operation of subsequent system equipment.
The filtered effluent enters a conditioning apparatus 400, typically a conditioning tank. As shown in fig. 2, a plurality of sewage mixing areas 410 are disposed in the adjusting device 400, a guide wall 4110 is disposed in each sewage mixing area 410, and flow pushers 4120 are disposed at two sides of the guide wall 4110. The adjusting device 400 adopts a gallery type water flow mode, sewage is subjected to hydraulic push flow stirring, the quality of the sewage is accelerated to be uniform, and the fluctuation of the quality of inlet water of the subsequent process is reduced. The water quality and the water quantity fluctuation of the comprehensive sewage in the chemical industry park are large, and the hydraulic retention time of the sewage in the adjusting device 400 is 6-8 hours.
The sewage with the uniform water quality by the adjusting device 400 enters the electrochemical oxidation unit 100 for electrochemical oxidation treatment, as shown in fig. 3, the electrochemical oxidation unit 100 is an electrochemical oxidation tower. Electric powerThe bottom of the chemical oxidation unit 100 is provided with a water distribution device 110, more than two electrochemical packing layers 120 are arranged in the electrochemical oxidation unit 100, and the height of each electrochemical packing layer 120 is 50-60 cm; the filler of the electrochemical filler layer 120 is composed of three parts, i.e., iron, carbon, and an active material, wherein the active material may be iron oxysulfate mineral, which is composed of four elements, i.e., Fe, O, S, and H, and has an average molecular formula of { Fe }8O8(OH)8-2x(SO4)x68 percent, 23 percent and 9 percent of each substance by mass respectively, the porosity is more than 60 percent, and the physical strength is 600kg/cm2The above; an internal circulation pipeline 130 is arranged at the top of the electrochemical oxidation unit 100, an internal circulation pump is arranged on the internal circulation pipeline 130, and the top of the electrochemical oxidation unit 100 is connected with the water distribution device 110 through the internal circulation pipeline 130. A water flow mode of downward inlet and upward outlet is adopted in the electrochemical oxidation tower, and the hydraulic retention time of the sewage in the electrochemical oxidation tower is controlled to be 2-3 h; and the pH value of the sewage in the tower is controlled to be maintained between 2.5 and 4 in the electrochemical oxidation treatment reaction process, and the reflux ratio of the sewage is controlled to be between 50 and 150 percent by controlling an internal circulating pump.
It should be noted that, under the acidic condition that the pH of the filler of the electrochemical filler layer 120 is 2.5-4, hydroxyl radicals can be rapidly generated by using the electrochemical principle, part of organic matters in the sewage can be removed by using the generated hydroxyl radicals, and macromolecular organic matters in the sewage can be decomposed into micromolecular organic matters, so that the biochemical performance of the sewage can be improved.
The sewage treated by the electrochemical oxidation unit 100 enters the fenton treatment unit 200 for fenton treatment. As shown in fig. 4, a fenton dosing area 210, a fenton reaction area 220 and a coagulation reaction area 230 are arranged in the fenton processing unit 200, the fenton reaction area 220 is arranged between the fenton dosing area 210 and the coagulation reaction area 230, and preferably, the volume ratio of the fenton dosing area 210, the fenton reaction area 220 and the coagulation reaction area 230 is (1-1.5): (7-10): (1-1.5); more preferably 1: 7: 1; an aeration device 240 is arranged in the Fenton reaction zone 220, stirring devices 250 are arranged in the Fenton dosing zone 210 and the coagulation reaction zone 230, the distance between each stirring device 250 and the bottom is 20-30 cm, and preferably, each stirring device 250 can be a double-slurry stirrer or a single-slurry stirrer; more preferably, a double paddle blender is provided within the fenton dosing section 210.
It should be noted that the region in the fenton dosing region 210 where the stirring device 250 is arranged is used as a 30% hydrogen peroxide dosing region, and the mass ratio of the oxidant dosing amount to the system water inflow is controlled to be (0.8-2.5): 1000 is less than the total weight of the product; in the Fenton reaction zone 220, the pH value is controlled to be 3-4 in the Fenton reaction process, and the reaction time is controlled to be 3-5 h. The pH value of the sewage treated by the Fenton reaction zone 220 is adjusted to 6-9, and then the sewage is subjected to PAM and/or PAC flocculation and precipitation treatment. The efficiency of the hydroxyl radicals generated by the Fenton reaction under the acidic condition is high, and the reaction rate of the generated hydroxyl radicals and the organic matters in the sewage can be improved and the removal rate of the organic matters in the sewage can be improved by utilizing the aeration stirring effect in the tank; the Fenton effluent meets the biochemical treatment condition, the acidic sewage needs to be regulated to be neutral, and physicochemical solid particles in the sewage are reduced through flocculation.
The electrochemical oxidation and Fenton methods both belong to advanced oxidation treatment processes, and the sewage in the chemical industrial park often contains refractory organic matters (such as pesticides, antibiotics and the like) with high toxicity, so that the water quality load of biochemical influent water at the rear end can be reduced through double advanced oxidation treatment, and the biochemical treatment effect is ensured to be good. And the front end electrochemical oxidation degradation treatment can reduce the dosage of the medicament in the rear end Fenton treatment process and reduce the generation amount of materialized sludge, thereby reducing the operation cost.
The biochemical treatment unit comprises a UBF pool, an A/O pool, a secondary sedimentation pool and a high-efficiency sedimentation pool in sequence. As shown in fig. 5, the UBF tank 310 is connected to the fenton treatment unit 200 through a pipe, and the sewage treated by the fenton treatment unit 200 enters the UBF tank to be treated. The water distribution pipe is arranged at the bottom of the UBF pool 310, water is distributed by adopting an upflow branch type, a support suspended filler zone 3110 is arranged in the UBF pool 310, the height of the support suspended filler zone 3110 is set to be 2.5-3 m, more than two triangular weir plates 3120 (shown in figure 6) are arranged at the top of the UBF pool 310 and are used for water discharge in a multi-groove water discharge mode, and the hydraulic retention time of sewage in the UBF pool 310 is 18-24 h.
The sewage treated by the UBF tank enters an A/O tank for treatment, the A/O tank comprises an anoxic tank and an aerobic tank, a filler layer is arranged in the anoxic tank, the filler layer accounts for 45-60% of the volume of the anoxic tank, the filler is made of spherical materials and comprises plastics and polyurethane, specifically, a spherical plastic frame is arranged outside the filler, and strip-shaped polyurethane is filled inside the filler. The total hydraulic retention time of the sewage in the A/O pool is controlled to be 24-28 h, wherein the hydraulic retention time in the anoxic pool and the hydraulic retention time in the aerobic pool are respectively 8-9 h and 16-19 h, and the reflux ratio of the sewage in the A/O pool is controlled to be 150-300%.
The sludge enters a secondary sedimentation tank for treatment after being treated by an A/O tank, the secondary sedimentation tank adopts a radial flow sedimentation tank structure, and a sludge scraper is arranged in the secondary sedimentation tank, preferably a central transmission sludge scraper; the sludge reflux ratio between the secondary sedimentation tank and the A/O tank is 50-150%, and the surface load of the secondary sedimentation tank is set to be 0.5-0.6.
And the sewage treated by the secondary sedimentation tank enters a high-efficiency sedimentation tank, a flocculation dosing area and a dephosphorization dosing area are arranged in the high-efficiency sedimentation tank, a flocculation medicament is one or two of PAC (polyaluminium chloride) and PAM (polyacrylamide), and the dosing mass ratio between the PAC dosing amount and the system water inflow is controlled to be (0.8-1): 100000, the phosphorus removal agent is a 40% calcium chloride solution, and the adding mass ratio between the adding amount of the calcium chloride solution and the water inflow of the system is controlled to be (0.5-1.5): 1000, the middle part of the high-efficiency sedimentation tank is provided with an inclined tube packing layer, and the height of the inclined tube packing layer is 1.2-1.5 m.
The sewage treated by the high-efficiency sedimentation tank can be directly discharged after reaching the standard; if not up to standard, sewage can get into activated carbon adsorption unit 500 and adsorb the processing, further degree of depth removes the pollutant in the sewage, ensures that sewage discharge up to standard. As shown in fig. 7, the activated carbon adsorption unit 500 is connected to the high-efficiency sedimentation tank through a pipeline, and the activated carbon adsorption unit 500 is generally an activated carbon adsorption tower, an activated carbon packing layer 510 is disposed in the adsorption tower, the height of the activated carbon packing layer 510 is 1.5-2.0 m, the particle size of the activated carbon packing is 1-2 cm, and the activated carbon adsorption tower is provided with a back-flushing pipeline 520 for back-flushing operation after adsorption.
The chemical industrial park comprehensive sewage treatment system is very suitable for treating the chemical industrial park comprehensive sewage with large water quality and water quantity fluctuation, difficult degradation and poor biodegradability, and the sewage is treated by a grating, a regulating tank, an electrochemical oxidation tower, a Fenton tank, a UBF tank, an A/O tank, a secondary sedimentation tank, a high-efficiency sedimentation tank and an activated carbon adsorption tower and then is discharged after reaching the standard; the biodegradability of sewage is improved while the degradation of refractory organic matters is degraded through a front-end advanced oxidation process, a high-quality living environment is provided for rear-end biochemical treatment microorganisms, and meanwhile, an activated carbon adsorption unit is arranged at the tail end to ensure that the sewage reaches the standard and can ensure that the quality of the effluent of a sewage plant stably reaches the first-level A discharge standard in the table 1 of the pollutant discharge standard of urban sewage treatment plant GB18918-2002 under the condition that the quality of the influent water meets the third-level discharge standard of the national Integrated wastewater discharge Standard GB 8978-1996.
The comprehensive sewage treatment process for the chemical industry park can efficiently and stably treat the comprehensive sewage of the chemical industry park, has the advantages of small process floor area, low operation cost and the like, and provides technical support for the regional environment treatment of the park in China.
Example 1
The comprehensive chemical wastewater discharged from a chemical park is treated, the influent COD is maintained between 350 and 500mg/L, the influent BOD is maintained between 30 and 50mg/L, the influent BOD/COD is lower than 0.1, the biodegradability is poor, the comprehensive chemical wastewater contains pesticide substances such as carbendazim, phosphorus trichloride and the like, the biological toxicity is high, the comprehensive chemical wastewater is difficult to degrade, and the rest water quality indexes TN, TP and NH are4 +the-N values are respectively 30-60 mg/L, 2-3.5 mg/L and 18-35 mg/L, and the specific operation process steps are as follows:
the comprehensive sewage in the chemical industry park passes through a mechanical grating, and the grating gap of the mechanical grating is 20 mm;
the sewage filtered by the grating enters an adjusting tank again, a gallery type water flow mode is adopted in the adjusting tank, submersible water flow pushers are installed on two sides of a flow guide wall, and the hydraulic retention time of the sewage in the adjusting tank is 6 hours;
the sewage after the water quality is homogenized by the regulating tank enters an electrochemical oxidation tower for treatment, the internal reflux ratio is 100 percent, and the electrochemistry in the tower is carried outThe filler consists of iron, carbon and active substances, the mass ratio of each substance is respectively 68%, 23% and 9%, the porosity is 63%, and the physical strength is 600kg/cm2The hydraulic retention time of the sewage in the electrochemical oxidation tower is 2 hours, and the pH value of the sewage in the tower is controlled to be 3.0 in the reaction process;
the sewage after the electrochemical oxidation tower treatment enters a Fenton pool again for treatment, an aeration system is arranged in a Fenton reaction area in the Fenton pool, the reaction time is 4 hours, the pH value is controlled to be 3.5 in the reaction process, a stirring area is arranged at the front end of the Fenton pool and is used as a 30% hydrogen peroxide adding area, and the mass ratio between the oxidant adding amount and the system water inflow amount is controlled to be 1.1: 1000, adjusting the pH value of the sewage treated by the Fenton pool to 7.5, and performing flocculation precipitation treatment by PAM and PAC;
the sewage after the Fenton pool and the flocculation precipitation treatment enters a UBF pool for treatment, the UBF pool distributes the water for the inlet water in an upstream branch type, a water distribution pipe is arranged at the bottom of the UBF pool, a packing layer is arranged in the middle of the UBF pool, the packing adopts a suspended soft combined packing, the height of the packing is set to be 2.5m, the hydraulic retention time of the sewage in the UBF pool is 20h, and the top of the pool body adopts a water outlet mode of two groups of parallel triangular weir plates;
the sewage treated by the UBF tank enters an A/O tank for treatment, wherein the A/O tank consists of an anoxic tank and an aerobic tank, spherical filler is added into the anoxic tank, the filling degree of the filler is controlled to be 50 percent (volume ratio), the total hydraulic retention time of the sewage in the A/O tank is controlled to be 26 hours, the hydraulic retention time in the anoxic tank and the hydraulic retention time in the aerobic tank are respectively 8 hours and 18 hours, and the reflux ratio of mixed liquid in the A/O tank is controlled to be 150 percent;
the sewage enters a secondary sedimentation tank for treatment after being treated by an A/O tank, the secondary sedimentation tank adopts a radial flow sedimentation tank structure form, a central transmission mud scraper device is adopted in the secondary sedimentation tank, the sludge reflux ratio between the secondary sedimentation tank and the A/O tank is controlled to be 100%, and the surface load of the secondary sedimentation tank is set to be 0.5;
the sewage treated by the secondary sedimentation tank enters a high-efficiency sedimentation tank, the high-efficiency sedimentation tank is provided with a flocculation dosing region and a dephosphorization dosing region, the flocculation reagents are PAC and PAM, and the mass ratio of the PAC dosing amount to the system water inflow is controlled to be 0.8: 100000, the phosphorus removal agent is a 40% calcium chloride solution, and the adding proportion between the adding amount of the calcium chloride solution and the water inflow of the system is controlled to be 0.8: 1000, arranging an inclined tube packing layer in the middle of the high-efficiency sedimentation tank, wherein the filling height of the inclined tube packing is 1.3 m;
the sewage enters an activated carbon adsorption tower for treatment after being treated by a high-efficiency sedimentation tank, granular activated carbon filler is filled in the activated carbon adsorption tower, the particle size is 1cm, the filling height is 1.8m, water enters from the bottom, water exits from the upper part, and a back flush pipeline is arranged;
the sewage is directly discharged to a discharge port after passing through an active carbon adsorption tower.
The detection result of the effluent quality of the process at each stage shows that: after the comprehensive sewage in the garden is treated by an electrochemical oxidation tower and Fenton, the removal rate of COD in the effluent reaches more than 60.5 percent, and the B/C ratio of the effluent reaches more than 0.3; the materialized effluent is treated by an A/O tank and a tail end efficient sedimentation tank, and the effluent quality COD, TN, TP and NH4 +N is respectively 55mg/L, 8mg/L, 0.3mg/L and 1.2mg/L, and only COD does not reach the discharge standard; the effluent of the high-efficiency sedimentation tank is treated by an activated carbon adsorption tower, and the effluent quality COD, TN, TP and NH4 +N is 45mg/L, 7.3mg/L, 0.25mg/L and 0.9mg/L respectively, and all reach the first grade A discharge standard in the pollutant discharge standard of urban sewage treatment plant GB18918-2002 Table 1.
Example 2
The comprehensive chemical wastewater discharged from a certain chemical park is treated, the influent COD is maintained between 400 and 500mg/L, the influent BOD is maintained between 35 and 50mg/L, the influent BOD/COD is lower than 0.1, the biodegradability is poor, and the rest water quality indexes of TN, TP and NH are4 +the-N values are respectively 45-65 mg/L, 3-4 mg/L and 20-40 mg/L, and the specific operation process steps are as follows:
the comprehensive sewage in the chemical industry park passes through a mechanical grating, and the grating gap of the mechanical grating is 20 mm;
the sewage filtered by the grating enters an adjusting tank again, a gallery type water flow mode is adopted in the adjusting tank, submersible water flow pushers are installed on two sides of a gallery, and the hydraulic retention time of the sewage in the adjusting tank is 8 hours;
water is homogenized by a regulating pondThe sewage after the treatment enters an electrochemical oxidation tower for treatment, the internal reflux ratio is 120 percent, electrochemical filler in the tower consists of iron, carbon and active substances, the mass ratio of the substances is respectively 68 percent, 23 percent and 9 percent, the porosity is 68 percent, and the physical strength is 600kg/cm2The hydraulic retention time of the sewage in the electrochemical oxidation tower is 2.5h, and the pH value of the sewage in the tower is controlled to be 3.5 in the reaction process;
the sewage after the electrochemical oxidation tower treatment enters a Fenton pool again for treatment, an aeration system is arranged in a Fenton reaction area in the Fenton pool, the reaction time is 4.5h, the pH value is controlled to be 3.5 in the reaction process, a stirring area is arranged at the front end of the Fenton pool and is used as a 30% hydrogen peroxide adding area, and the mass ratio of the oxidant adding amount to the system water inflow amount is controlled to be 1.5: 1000, adjusting the pH value of the sewage treated by the Fenton pool to 7.0, and performing flocculation precipitation treatment by PAM and PAC;
the sewage after the Fenton pool and the flocculation precipitation treatment enters a UBF pool for treatment, the UBF pool distributes the water for the inlet water in an upstream branch type, a water distribution pipe is arranged at the bottom of the UBF pool, a packing layer is arranged in the middle of the UBF pool, the packing adopts a suspended soft combined packing, the height of the packing is set to be 3m, the hydraulic retention time of the sewage in the UBF pool is 24h, and the top of the pool body adopts a water outlet mode of two groups of parallel triangular weir plates;
the sewage treated by the UBF tank enters an A/O tank for treatment, wherein the A/O tank consists of an anoxic tank and an aerobic tank, spherical filler is added into the anoxic tank, the filling degree of the filler is controlled to be 50 percent (volume ratio), the total hydraulic retention time of the sewage in the A/O tank is controlled to be 28 hours, the hydraulic retention time in the anoxic tank and the hydraulic retention time in the aerobic tank are respectively 9 hours and 19 hours, and the reflux ratio of mixed liquid in the A/O tank is controlled to be 200 percent;
the sewage enters a secondary sedimentation tank for treatment after being treated by an A/O tank, the secondary sedimentation tank adopts a radial flow sedimentation tank structure form, a central transmission mud scraper device is adopted in the secondary sedimentation tank, the sludge reflux ratio between the secondary sedimentation tank and the A/O tank is controlled to be 120 percent, and the surface load of the secondary sedimentation tank is set to be 0.5;
the sewage treated by the secondary sedimentation tank enters a high-efficiency sedimentation tank, the high-efficiency sedimentation tank is provided with a flocculation dosing region and a dephosphorization dosing region, a flocculation medicament is PAC and PAM, and the mass ratio of the PAC dosing amount to the system water inflow is controlled to be 1: 100000, the phosphorus removal agent is a 40% calcium chloride solution, and the adding proportion between the adding amount of the calcium chloride solution and the water inflow of the system is controlled to be 1.2: 1000, arranging an inclined tube packing layer in the middle of the high-efficiency sedimentation tank, wherein the filling height of the inclined tube packing is 1.5 m;
the sewage can enter an activated carbon adsorption tower for further treatment after being treated by a high-efficiency sedimentation tank, granular activated carbon filler is filled in the activated carbon adsorption tower, the particle size is 1.5cm, the filling height is 2m, water enters from the bottom, water exits from the upper part, and a back flush pipeline is arranged.
The detection result of the effluent quality of the process at each stage shows that: after the comprehensive sewage in the garden is treated by an electrochemical oxidation tower and Fenton, the removal rate of COD in the effluent reaches over 64.5 percent, and the B/C ratio of the effluent reaches over 0.35; the materialized effluent is treated by an A/O tank and a tail end efficient sedimentation tank, and the effluent quality COD, TN, TP and NH4 +N is 41mg/L, 10.1mg/L, 0.15mg/L and 0.73mg/L respectively, and all reach the first grade A discharge standard in the pollutant discharge standard of urban sewage treatment plant GB18918-2002 Table 1.
The present invention and its embodiments have been described above schematically, the description is not restrictive, the data used are only one of the embodiments of the present invention, and the actual data combination is not limited to this. Therefore, if the person skilled in the art receives the teaching, the embodiments and examples similar to the above technical solutions shall not be designed in an inventive manner without departing from the spirit of the present invention, and shall fall within the protection scope of the present invention.

Claims (10)

1. The utility model provides a sewage treatment system is synthesized in chemical industry garden which characterized in that: the device comprises an electrochemical oxidation unit (100), a Fenton processing unit (200) and a biochemical processing unit, wherein the Fenton processing unit (200) is arranged between the electrochemical oxidation unit (100) and the biochemical processing unit, the front end of the electrochemical oxidation unit (100) is provided with a regulating device (400), and the regulating device (400) is connected with the electrochemical oxidation unit (100) through a pipeline; wherein the content of the first and second substances,
the bottom of the electrochemical oxidation unit (100) is provided with a water distribution device (110), more than two electrochemical packing layers (120) are arranged in the electrochemical oxidation unit (100), the top of the electrochemical oxidation unit (100) is provided with an internal circulation pipeline (130), and the top of the electrochemical oxidation unit (100) is connected with the water distribution device (110) through the internal circulation pipeline (130);
a Fenton dosing area (210), a Fenton reaction area (220) and a coagulation reaction area (230) are arranged in the Fenton treatment unit (200), the Fenton reaction area (220) is arranged between the Fenton dosing area (210) and the coagulation reaction area (230), an aeration device (240) is arranged in the Fenton reaction area (220), and stirring devices (250) are arranged in the Fenton dosing area (210) and the coagulation reaction area (230);
the biochemical treatment unit comprises a UBF pool (310), an A/O pool, a secondary sedimentation pool and a high-efficiency sedimentation pool in sequence, wherein the UBF pool (310) is connected with the Fenton treatment unit (200) through a pipeline, a support suspension type packing area (3110) is arranged in the UBF pool (310), and more than two triangular weir plates (3120) are arranged at the top of the UBF pool (310); and is
A plurality of sewage mixing areas (410) are arranged in the adjusting device (400), guide walls (4110) are arranged in the sewage mixing areas (410), and flow pushers (4120) are arranged at positions on two sides of each guide wall (4110).
2. The chemical industrial park integrated sewage treatment system according to claim 1, which is characterized in that: in the Fenton treatment unit (200), the volume ratio of a Fenton dosing zone (210), a Fenton reaction zone (220) and a coagulation reaction zone (230) is (1-1.5): (7-10): (1-1.5).
3. The chemical industrial park integrated sewage treatment system according to claim 1, which is characterized in that: the distance between the stirring device (250) arranged in the Fenton dosing area (210) and the coagulation reaction area (230) and the bottom is 20 cm.
4. The chemical industrial park integrated sewage treatment system according to claim 1, which is characterized in that: the height of a support suspension type filler area (3110) arranged inside the UBF pool (310) is 2.5-3 m.
5. The chemical industrial park integrated sewage treatment system according to claim 1, which is characterized in that: the adjusting device (400) is provided with a grating in front, and the gap of the grating is 16-25 mm.
6. The integrated sewage treatment system for chemical industrial park according to any one of claims 1 to 5, wherein: still include active carbon adsorption unit (500), active carbon adsorption unit (500) link to each other with high-efficient sedimentation tank through the pipeline, are provided with active carbon packing layer (510) in active carbon adsorption unit (500), and the height of active carbon packing layer (510) is 1.5 ~ 2.0m to active carbon adsorption unit (500) are provided with back flush pipeline (520), and the back flush process adopts the washing, and the rivers direction is for advancing from top to bottom and goes out.
7. A process for treating the sewage in chemical industrial park includes such steps as filtering the sewage by grate to remove impurities; the filtered sewage enters a regulating device for uniform water quality mixing treatment to obtain sewage with uniform water quality; the sewage with uniform water quality enters an electrochemical oxidation unit for electrochemical oxidation treatment, and macromolecular organic matters in the sewage are decomposed into micromolecular organic matters; the sewage after electrochemical oxidation treatment enters a Fenton treatment unit for Fenton treatment, so that refractory organic matters in the sewage are further removed, the water quality load of the sewage is reduced, and favorable conditions are provided for back-end biochemical treatment; and then the sewage after Fenton treatment enters a biochemical treatment unit, and is subjected to biochemical treatment in a UBF pool, an A/O pool, a secondary sedimentation pool and a high-efficiency sedimentation pool in sequence to obtain the sewage which reaches the discharge standard.
8. The chemical industrial park comprehensive sewage treatment process according to claim 7, which is characterized in that: and the sewage after biochemical treatment enters an activated carbon adsorption unit for adsorption treatment to obtain the sewage which reaches the discharge standard.
9. The chemical industrial park comprehensive sewage treatment process according to claim 7, which is characterized in that:
controlling the hydraulic retention time of the sewage in the electrochemical oxidation unit to be 2-3 h, controlling the pH value of the sewage in the electrochemical oxidation treatment reaction process to be 2.5-4, and controlling the reflux ratio of the sewage to be 50-150%;
or controlling the reaction time of the sewage in the Fenton reaction zone to be 3-5 h, controlling the pH value in the reaction process to be 3-4, and controlling the mass ratio of the adding amount of the oxidant added in the Fenton adding zone to the water inflow of the system to be (0.8-2.5): 1000.
10. The chemical industrial park comprehensive sewage treatment process according to claim 7, which is characterized in that:
controlling the hydraulic retention time of the sewage in the UBF pool to be 18-24 h, controlling the hydraulic retention time of the sewage in the anoxic pool to be 8-9 h, and controlling the hydraulic retention time in the aerobic pool to be 16-19 h;
or controlling the sewage reflux ratio in the A/O pool to be between 150 and 300 percent, and controlling the sludge reflux ratio between the secondary sedimentation pool and the A/O pool to be between 50 and 150 percent;
or the flocculation reagent added into a flocculation reagent adding area arranged in the high-efficiency sedimentation tank is one or two of PAC (polyaluminium chloride) and PAM (polyacrylamide), wherein the mass ratio of the adding amount of the flocculation reagent to the water inflow of the system is controlled to be (0.8-1): 100000; the phosphorus removal agent added in the phosphorus removal agent adding region is a calcium chloride solution with the concentration of 40%, and the mass ratio of the adding amount of the phosphorus removal agent to the water inflow of the system is controlled to be (0.5-1.5): 1000.
CN202110568580.4A 2021-05-25 2021-05-25 Chemical industry park comprehensive sewage treatment system and process Pending CN113511777A (en)

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